EP3896141B1 - Procédé de contrôle de la viscosité cinématique d'une polyalphaoléfine - Google Patents

Procédé de contrôle de la viscosité cinématique d'une polyalphaoléfine Download PDF

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EP3896141B1
EP3896141B1 EP21168133.3A EP21168133A EP3896141B1 EP 3896141 B1 EP3896141 B1 EP 3896141B1 EP 21168133 A EP21168133 A EP 21168133A EP 3896141 B1 EP3896141 B1 EP 3896141B1
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oligomerization
monomer
polyalphaolefin
halide
promoter
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EP3896141A1 (fr
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Sukhdeep Kaur
Usharani SAHOO
Gurmeet Singh
Naresh Pappu
Jai Narayan Pandey
Shobhashankar Kumhar
Gurpreet Singh Kapur
Deepak Saxena
Sankara Sri Venkata Ramakumar
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Indian Oil Corp Ltd
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Indian Oil Corp Ltd
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M107/00—Lubricating compositions characterised by the base-material being a macromolecular compound
    • C10M107/02—Hydrocarbon polymers; Hydrocarbon polymers modified by oxidation
    • C10M107/10—Hydrocarbon polymers; Hydrocarbon polymers modified by oxidation containing aliphatic monomer having more than 4 carbon atoms
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/02—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons
    • C07C2/04—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation
    • C07C2/06—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation of alkenes, i.e. acyclic hydrocarbons having only one carbon-to-carbon double bond
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/02—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons
    • C07C2/04—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation
    • C07C2/06—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation of alkenes, i.e. acyclic hydrocarbons having only one carbon-to-carbon double bond
    • C07C2/08—Catalytic processes
    • C07C2/14—Catalytic processes with inorganic acids; with salts or anhydrides of acids
    • C07C2/20—Acids of halogen; Salts thereof ; Complexes thereof with organic compounds
    • C07C2/22—Metal halides; Complexes thereof with organic compounds
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
    • C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
    • C07C2/66—Catalytic processes
    • C07C2/68—Catalytic processes with halides
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F110/00—Homopolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F110/14—Monomers containing five or more carbon atoms
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10M—LUBRICATING COMPOSITIONS; USE OF CHEMICAL SUBSTANCES EITHER ALONE OR AS LUBRICATING INGREDIENTS IN A LUBRICATING COMPOSITION
    • C10M2205/00—Organic macromolecular hydrocarbon compounds or fractions, whether or not modified by oxidation as ingredients in lubricant compositions
    • C10M2205/02—Organic macromolecular hydrocarbon compounds or fractions, whether or not modified by oxidation as ingredients in lubricant compositions containing acyclic monomers
    • C10M2205/028—Organic macromolecular hydrocarbon compounds or fractions, whether or not modified by oxidation as ingredients in lubricant compositions containing acyclic monomers containing aliphatic monomers having more than four carbon atoms
    • C10M2205/0285—Organic macromolecular hydrocarbon compounds or fractions, whether or not modified by oxidation as ingredients in lubricant compositions containing acyclic monomers containing aliphatic monomers having more than four carbon atoms used as base material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10N—INDEXING SCHEME ASSOCIATED WITH SUBCLASS C10M RELATING TO LUBRICATING COMPOSITIONS
    • C10N2010/00—Metal present as such or in compounds
    • C10N2010/06—Groups 3 or 13
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10N—INDEXING SCHEME ASSOCIATED WITH SUBCLASS C10M RELATING TO LUBRICATING COMPOSITIONS
    • C10N2020/00—Specified physical or chemical properties or characteristics, i.e. function, of component of lubricating compositions
    • C10N2020/01—Physico-chemical properties
    • C10N2020/02—Viscosity; Viscosity index

Definitions

  • the present disclosure relates to a method of oligomerization of C 6 and above olefin monomer to polyalphaolefin (PAO) using aluminum halide as catalyst along with a promoter. More specifically, the present disclosure relates to a method of controlling the kinematic viscosity of polyalphaolefins by adjusting the oligomerization temperature at fixed monomer/aluminum halide mole ratios.
  • polyalphaolefins which are used as synthetic base oils for lubricant applications.
  • Polyalphaolefins are used in many synthetic products such as lubricants, greases and fluids, and have emerged as essential components in many industries and applications.
  • Polyalphaolefins are specially designed chemicals that are uniquely made from alpha olefins.
  • the increase in polyalphaolefins applications is largely driven by the stability of the polyalphaolefins molecules. This stability, along with a host of other unique performance characteristics, makes polyalphaolefins far superior to mineral oils in a variety of uses.
  • Polyalphaolefins may be produced by using olefin as the feed and using BF 3 and AlCl 3 along with promoter as catalyst.
  • the evaluation of polyalphaolefins to various test conditions is carried out only after hydrogenation of polyalphaolefins is performed after oligomerization.
  • polyalphaolefins in the range of from 4 to 6 cSt, are typically made by oligomerization of 1-decene using a BF 3 catalyst and an alcohol promoter.
  • olefin feed used for oligomerization is 1-octene, 1-decene, 1-dodecene, 1-tetradecene and where possible mixtures also but the preferred olefin is 1-decene.
  • US 9708549 describes the method for oligomerizing olefin or for producing polyalphaolefin utilizing catalyst mixtures comprising aluminum halides and an organic liquid carrier where the organic liquid carrier comprises of at least 75 mole % 1,2-disubstituted olefins, trisubstituted olefins, or any combination thereof.
  • This patent teaches that stable liquid solutions can be formed between aluminum halides and an organic liquid carrier which can be prepared in advance of its use and stored for long periods of time.
  • US 5196635 describes the preparation of olefin oligomers by polymerizing one or a mixture of olefins, in the presence of a catalyst prepared by reacting in an organic solvent an aluminum halide and proton donor.
  • the olefin oligomer produced is having a kinematic viscosity of from about 30 to 400 cSt at 100° C.
  • US 5463158 describes a process for the catalytic oligomerization of light olefins, such as ethylene or propylene using a liquid catalyst which comprises a Lewis acid and a Lewis base component which forms with the Lewis acid a melt which is liquid at room temperature.
  • the Lewis acid is a metal halide, such as aluminum trichloride and the Lewis base is an organic salt, such as an organic halide salt containing an N-heterocyclic ring or salts containing fully substituted onium ions.
  • US 5451704 describes a process for the production of hydrocarbon lubricant base stock comprises contacting C2 to C20 alpha-olefin feedstock, or mixtures under heterogeneous oligomerization conditions with AlCl 3 anchored on an adsorbent inorganic oxide solid, e.g., silica.
  • US 4219691 describes a process for producing olefin oligomer from olefins having not less than 6 carbon atoms in the presence of a reaction mixture of an aluminum halide and a secondary or tertiary alcohol in equivalent proportions.
  • the olefin oligomers thus obtained have a high kinematic viscosity, a low pour point, a high viscosity index and a good shear stability. It also discloses that even if the reaction ratio of the aluminum halide and the secondary or tertiary alcohol is changed within the above-mentioned range, the kinematic viscosity of the oligomers so obtained is not greatly changed.
  • US8865959B2 relates to a process to produce a poly alpha-olefin (PAO) comprising: a) contacting one or more C4 to C24 alpha olefin monomers with a metallocene compound, and optionally an activator to produce a low molecular weight PAO comprising a mixture of oligomers having a number average molecular weight in the range of 120 to 600 and containing a terminal olefin content of at least 25 wt % of total olefinic unsaturation, and b) subsequently contacting at least a portion of said low molecular weight PAO with a Lewis acid catalyst and optionally one or more C4 to C24 alpha olefin monomers to produce a liquid PAO, wherein said liquid PAO has a mass average molecular weight of at least 988.
  • PAO poly alpha-olefin
  • US10435491 relates to a process comprising; contacting i) a monomer comprising a C6 to C20 olefin, ii) a haloaluminate ionic liquid, and iii) a halide component comprising a C1 to C12organohalide in a reaction zone; and oligomerizing the monomer in the reaction zone to form an oligomer product; wherein the oligomer product has an average molecular weight from 400 to 611 grams/mol, wherein the oligomer product is formed in a presence of less than 8 mol % isoparaffin based upon moles of monomer in the reaction zone, wherein a molar ratio of a halide in the halide component to an aluminum in the haloaluminate ionic liquid is at least 0.14:1, and wherein the oligomer product is formed at a temperature from 15°C. to 125°C.
  • CN106957677 provides a method for synthesizing low-viscosity PAO4 by high-purity linear alpha olefine through anhydrous AlCl3.
  • the method is characterized in that, in a hot 1-decene monomer, a catalyst is dropwise added, and then low-viscosity PAO4 base oil is synthesized, wherein the catalyst is selected from aluminium chloride anhydrous; the hot 1-decene monomer is heated to 90 DEG C or above.
  • the disclosure provides the method for synthesizing the low-viscosity PAO4 by the high-purity linear alpha olefine through the anhydrous AlCl 3 .
  • the industrial catalyst adopted by the method is low-price; the catalyst is easily obtained; further, the catalyst in a reaction process is easily treated; the reaction condition is mild; the low-viscosity PAO obtained through preparation is good in viscosity temperature characteristic.
  • US7550640 relates to the use of 1-decene/1-dodecene olefin mixture to produce high viscosity polyalphaolefins (PAOs) having a viscosity of from about 40 cSt to about 100 cSt at 100°C. (ASTM D-445) and a number average molecular weight of between about 1200 to about 4000, particularly useful as lubricant base stocks.
  • PAOs polyalphaolefins
  • US7880047B2 relates to polyalphaolefins and processes and reaction systems for forming polyalphaolefins from an ⁇ -olefin, preferably a C8-C12 ⁇ -olefin such as 1-decene, by co-feeding to the polymerization reaction mixture a C8-C12 saturated hydrocarbon, preferably having the same number of carbon atoms as the ⁇ -olefin.
  • ⁇ -olefin preferably a C8-C12 ⁇ -olefin such as 1-decene
  • US8067652B2 relates to a process for forming a polyalphaolefin, the process comprising the step of polymerizing at least one C8-C12 monomer, preferably a decene such as 1-decene, in the presence of an aluminoxane, an activator and a metallocene to form the polyalphaolefin, wherein the molar ratio of the aluminoxane to the metallocene is less than 250:1.
  • US7259284B2 relates to a continuous process for the manufacture of high viscosity polyalphaolefin products from an alpha olefin feedstock using an ionic liquid catalyst where the polyalphaolefin products have unique physical properties that make them useful as lubricants or lubricant additives.
  • US8207390B2 relates to a process to produce poly-alpha-olefins (PAOs) in the presence of a metallocene catalyst with a non-coordinating anion activator and hydrogen.
  • PAOs poly-alpha-olefins
  • US4031159A relates to a method of preparing polyolefin oils which can practically or perfectly prevent halogen from getting mixed in the polymerization product and produce a polyolefin oil having a relatively low viscosity and a high viscosity index at a high yield.
  • the method as disclosed herein covers two methods of preparing polyolefin oils, and one of said methods comprises polymerizing an olefin having 6 or more carbon atoms in the presence of a mixture of (a) a polyester obtained by esterifying all the carboxyl groups of a carboxylic acid having 2 to 20 carbon atoms with aliphatic saturated alcohol having 1 to 20 carbon atoms and (b) an aluminum halide in an amount of 0.7 to 2.0 moles per 1 ester bond of said polyester.
  • a polyolefin oil which scarcely contains halogen and has a viscosity in the range of about 40 - 90 centistokes and a viscosity index (VIE) of 130 or more can be obtained at a yield of 83% or more.
  • US4041098A relates to a method of oligomerizing straight chain alpha olefins having at least 3 carbon atoms comprising, generating in situ a soluble catalyst system by simultaneously adding with stirring to a reactor having an inert atmosphere and a temperature up to 200° C., a first feed comprising a straight chain alpha-olefin monomer having at least 3 carbon atoms and a minor amount of a soluble aluminum alkyl halide and a second feed comprising a straight chain alpha-olefin monomer having at least three carbon atoms and a minor amount of a soluble organic halide; wherein said soluble aluminum alkyl halide compound is selected from the group consisting of ethyl aluminum sesqui-chloride, ethyl aluminum dichloride and diethyl aluminum chloride, and said soluble organic halide is selected from the group consisting of a primary, secondary or tertiary aliphatic halide, an allylic hal
  • the present disclosure provides a method of controlling the kinematic viscosity of polyalphaolefins by adjusting the oligomerization temperature at fixed monomer/aluminum halide mole ratios.
  • It is a primary objective of the disclosure which relates to a method of the oligomerization of C 6 and above olefin monomer whereby, at a fixed monomer/Al halide mole ratio, polyalphaolefins having desirable kinematic viscosities are prepared by controlling the oligomerization temperature.
  • the oligomerization is carried out in presence of an oligomerizing catalyst comprising of aluminum halide and a promoter, and oligomerizing temperatures of about 10°C to about 120°C.
  • an object of the present disclosure is that the oligomer obtained has Br number is > 0.2. It is a further objective of the present disclosure to obtain the oligomer with improved viscosity index.
  • the present disclosure discloses a process for controlling kinematic viscosity of a polyalphaolefin below 70 centistokes , the process comprising the steps of oligomerizing C 6 and above olefin monomers in the presence of an aluminum halide, a promoter and optionally, a solvent to obtain a polyalphaolefin; wherein, the kinematic viscosity of the polyalphaolefin is controlled by adjusting oligomerization temperature at a fixed monomer and aluminium halide mole ratio.
  • the olefin monomer or monomer is selected from the group comprising of 1-decene, 1-dodecene, 1-octene and any mixtures thereof.
  • mole ratio of the olefin monomer or monomer to the aluminum halide is from 10 to 500, more preferably from 10 to 350, most preferably from 40 to 300.
  • mole ratio of the aluminum halide to the promoter is from 1 to 10, preferably from 1 to 5.
  • the promoter is iso-butyl alcohol.
  • the olefin monomers or monomers and the solvents have moisture content less than 20 ppm.
  • the oligomerization temperature is in the range from 10° C to 150° C.
  • the oligomerization temperature is 25°C and 90°C.
  • residence time during the oligomerization is in the range of 0.5 to 8 hours.
  • the solvent is selected from C5 to C19 paraffinic hydrocarbons.
  • conversion from the olefin monomer or monomer to polyalphaolefin is greater than 95%.
  • the oligomerization comprises C20-24 dimers, C30-36 trimers, C40-48 tetramers, C50-60 pentamers, and C60+ heavies.
  • the disclosure relates to a method of the oligomerization of C6 and above olefin monomer whereby, at a fixed monomer/Al halide mole ratio, polyalphaolefins having desirable kinematic viscosities are prepared by controlling the oligomerization temperature.
  • the oligomerization is carried out in presence of an oligomerizing catalyst comprising of aluminum halide and a promoter, and oligomerizing temperatures of about 10°C to about 120°C.
  • a method of oligomerization of C 6 and above olefin monomer to polyalphaolefin having desirable kinematic viscosity comprising of the step of oligomerizing in the presence of an aluminum halide and a promoter, wherein the mole ratio of the monomer to the aluminum halide is from 10 to 500, preferably from 10 to 350.
  • halide can be chloride, bromide or iodide, preferably chloride or bromide.
  • the aluminum halide is aluminum chloride or aluminum bromide.
  • C 6 and above olefin monomer can be olefins of the range C 6 to C 14 , wherein, mixtures of C 6 to C 14 olefin monomer can be used. In another embodiment, recycle or redistilled olefin monomer can be used.
  • the disclosure relates to a process for oligomerization of and above olefin monomer to polyalphaolefin having desirable kinematic viscosity, the process comprising of the step of oligomerizing in the presence of an aluminum halide and a promoter, wherein the mole ratio of the aluminum halide to the promoter is from 1 to 10, preferably from 1 to 5.
  • the promoter is iso-butyl alcohol.
  • the inventors were surprised to find that by controlling the oligomerization temperature, at a fixed monomer/Al weight ratio, polyalphaolefins having desirable kinematic viscosities are prepared.
  • the oligomerization temperature is in the range from 10° C to 150° C, although temperatures outside this range can be utilized.
  • the preferred oligomerization temperature is 10° C to 120° C.
  • heat transfer capability may be necessary for non-adiabatic oligomerizations, to maintain steady state conditions.
  • the residence time over which the oligomer product is formed is the time where desired conversions are achieved. In an embodiment, the residence time during oligomerization of about 0.5 to 8 h.
  • the reactants as well as the apparatus/equipments should be poison free especially air and moisture.
  • all the apparatus/equipments are heated and dried either in vacuum or nitrogen while monomers and solvents are distilled, passed through dessicant columns or stored over dessicants.
  • Manipulation before and during oligomerizations for maintaining inert conditions and atmospheres are carried out wherever necessary.
  • no solvent is used during the oligomerization.
  • the choice of solvent can be related to the oligomerization temperature.
  • the solvent can be selected from C 5 to C 19 paraffinic hydrocarbons.
  • the conversion from the monomer to oligomer is normally greater than 95%.
  • the oligomerization is stopped by addition of water or alcohol, followed by a catalyst removal step, such as an aqueous wash or filtration, absorption or centrifugation.
  • the next step is removal of monomer, promoter and low boiling oligomers through distillation.
  • the oligomeric product is essentially hydrogenated but can be optionally either before or after distillation.
  • the hydrogenation is carried out using metallic catalyst and hydrogen. Normally, bromine number below 5 and more preferably below 2 will produce an oligomer with excellent oxidation stability.
  • the resulting product is typically hydrogenated to saturate the oligomers to provide a product having a desired viscosity, for example 40 cSt or 100 cSt at 100° C.
  • the product of the oliogmerization typically comprises C 20-24 dimers, C 30-36 trimers, C 40-48 tetramers, C 50-60 pentamers, and C 60 + heavies.
  • the oligomerized product can be used in variety of application for example, as base oils in lubricants, additives for various compositions, viscosity index improvers, dispersants etc.
  • AlCl 3 based chemistry is extensively used to produce PAO.
  • the variation of reactant mol ratios, effect of varying the substituents or solvents have been extensively studied.
  • PAO of different viscosities are prepared. This itself is unique especially for preparing low viscosities PAO as each batch can be tuned to produce, e.g., PAO4 in high concentration.
  • Each batch will produce PAO from dimers to pentamers which can be separated by distillation.
  • the kinematic viscosity (sometimes also called the momentum diffusivity), defined as the ratio of the viscosity ⁇ to the density of the fluid ⁇ . It is usually denoted by the Greek letter nu (v) and has dimension (length)2/time.
  • SVM 3000 Stabinger Viscometer is used to measure the dynamic viscosity and density of oils and fuels according to ASTM D7042-21. From said dynamic viscosity results/values, the SVM 3000 viscometer automatically calculates the kinematic viscosity and delivers measurement results which are equivalent to ISO 3104 or ASTM D445-19a.
  • the dynamic viscosity is the essential value for evaluating the lubricating behavior.
  • Viscosity index is a dimensionless number and is used to investigate the change in the viscosity at different temperatures. The greater the viscosity index (VI), the smaller the change in fluid viscosity for a given change in temperature, and vice versa. The viscosity index is calculated from the kinematic viscosity at different temperature ranges.
  • the present disclosure discloses a process for controlling kinematic viscosity of a polyalphaolefin below 70 centistokes, the process comprising the steps of oligomerizing C6 and above olefin monomers in the presence of an aluminum halide, a promoter and optionally, a solvent to obtain a polyalphaolefin; wherein, the kinematic viscosity of the polyalphaolefin is controlled by adjusting oligomerization temperature at a fixed monomer and aluminium halide mole ratio.
  • the present disclosure discloses a process for controlling kinematic viscosity of a polyalphaolefin in a range of 1-70 centistokes, the process comprising the steps of: oligomerizing C6 and above olefin monomers in the presence of an aluminum halide, a promoter and optionally, a solvent to obtain a polyalphaolefin; wherein, the kinematic viscosity of the polyalphaolefin is controlled by adjusting oligomerization temperature at a fixed monomer and aluminium halide mole ratio.
  • the olefin monomer or monomer is selected from the group comprising of 1-decene, 1-dodecene, 1-octene and any mixture thereof.
  • mole ratio of the olefin monomer or monomer to the aluminum halide is from 10 to 500, more preferably from 10 to 350, most preferably from 40 to 300.
  • mole ratio of the aluminum halide to the promoter is from 1 to 10, preferably from 1 to 5.
  • the promoter is iso-butyl alcohol.
  • the olefin monomers or monomers and the solvents have moisture content less than 20 ppm.
  • the oligomerization temperature is in the range from 10° C to 150° C.
  • the oligomerization temperature is 25°C and 90°C.
  • residence time during the oligomerization is in the range of 0.5 to 8 hours.
  • the solvent is selected from C5 to C19 paraffinic hydrocarbons.
  • conversion from the monomer to polyalphaolefin is greater than 95%.
  • the oligomerization comprises C20-24 dimers, C30-36 trimers, C40-48 tetramers, C50-60 pentamers, and C60+ heavies.
  • the kinematic viscosity decreases on increasing the monomer and the aluminium halide mole ratio.
  • the hydrogenation is carried out using metallic catalyst and hydrogen.
  • conversion from the monomer to oligomer is greater than 95%.
  • the present disclosure discloses a process for preparing a polyalphaolefin, the process comprising the steps of a) oligomerizing C6 and above olefin monomers under an inert atmosphere in the presence of an aluminum halide, a promoter and optionally, a solvent to obtain an oligomeric product, i.e., polyalphaolefin; wherein kinematic viscosity of the polyalphaolefin is below 70 centistokes.
  • Table 1 showing the effect of temperature on the viscosity of the PAO at fixed Monomer/Al ratios Monomer/A1 ratio KV@100°C % Conversion Oligomerization Temp 25°C Oligomerization Temp 90°C 10 61.1 30.9 95 25 60.1 30.2 97 48 53.9 25.4 98 83 45.6 23.6 98 100 30.4 8.1 96 165 23.4 5.8 96 282 12.1 4.5 95 450 8.6 3.2 96 Table 2 showing the effect of fixing the Monomer/Al ratios during runaway reaction Monomer/A1 ratio KV@100°C % Conversion Oligomerization Temperature 25°C Runaway Reaction Temperature 100 - 110°C 10 61.1 12.9 95 83 45.6 10.9 98 100 30.4 6.5 96 165 23.4 4.0 96 282 12.1 2.1 95
  • the procedure for oligomerization followed was same as described in Example 1 but instead, the oligomerization temperature was set to 90°C.
  • the hydrogenated oil had KV of 23.5 cSt @100°C, VI of 147.
  • the procedure for oligomerization followed was same as described in Example 1 but instead, the C10/AlCl 3 mol ratio was kept as 282.
  • the hydrogenated oil had KV of 12.1 cSt @100°C, VI of 142.
  • the procedure for oligomerization followed was same as described in Example 1 but instead, the C10/AlCl 3 mol ratio was kept as 282 and the oligomerization temperature was set to 90°C.
  • the hydrogenated oil had KV of 4.5 cSt @100°C, VI of 142.
  • the procedure for oligomerization followed was same as described in Example 1 but instead, the C10/AlCl 3 mol ratio was kept as 165.
  • the hydrogenated oil had KV of 23.4 cSt @100°C, VI of 142.
  • the procedure for oligomerization followed was same as described in Example 1 but instead, the C10/AlCl 3 mol ratio was kept as 165 and the oligomerization temperature was set to 90°C.
  • the hydrogenated oil had KV of 5.8 cSt @100°C, VI of 144.
  • the procedure for oligomerization followed was same as described in Example 1 but instead, the C10/AlCl 3 mol ratio was kept as 100.
  • the hydrogenated oil had KV of 30.4 cSt @100°C, VI of 142.
  • the procedure for oligomerization followed was same as described in Example 1 but instead, the C10/AlCl 3 mol ratio was kept as 100 and the oligomerization temperature was set to 90°C.
  • the hydrogenated oil had KV of 8.1 cSt @100°C, VI of 141.
  • the procedure for oligomerization followed was same as described in Example 1 but instead, the monomer/AlCl 3 mol ratio was kept as 48 and the monomer was 1-dodecene, and the oligomerization temperature was set to 90°C.
  • the hydrogenated oil had KV of 25.4 cSt @100°C, VI of 142.

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Claims (10)

  1. Procédé de contrôle de la viscosité cinématique d'une polyalphaoléfine dans une plage de 1 à 70 centistokes à 100°C, le procédé comprenant les étapes suivantes :
    l'oligomérisation de monomères d'oléfines C6 et supérieures en présence d'un halogénure d'aluminium, d'un promoteur et éventuellement d'un solvant pour obtenir une polyalphaoléfine ;
    dans lequel la viscosité cinématique de la polyalphaoléfine est contrôlée en ajustant la température d'oligomérisation à un rapport molaire fixe entre le monomère oléfine et l'halogénure d'aluminium,
    dans lequel le rapport molaire entre le monomère d'oléfine et l'halogénure d'aluminium est compris entre 10 et 500 ;
    dans lequel la température d'oligomérisation est comprise entre 10°C et 150°C ;
    dans lequel le promoteur est l'alcool iso-butylique ; et
    dans lequel le rapport molaire entre l'halogénure d'aluminium et le promoteur est compris entre 1 et 10.
  2. Procédé selon la revendication 1, dans lequel le monomère oléfine est choisi dans le groupe comprenant le 1-décène, le 1-dodécène, le 1-octène et tout mélange de ceux-ci.
  3. Procédé selon la revendication 1, dans lequel le rapport molaire entre le monomère oléfine et l'halogénure d'aluminium est compris entre 10 et 350, de préférence entre 40 et 300.
  4. Procédé selon la revendication 1, dans lequel le rapport molaire entre l'halogénure d'aluminium et le promoteur est compris entre 1 et 5.
  5. Procédé selon la revendication 1, dans lequel les monomères et les solvants ont une teneur en humidité inférieure à 20 ppm.
  6. Procédé selon la revendication 1, dans lequel la température d'oligomérisation est comprise entre 25°C et 90°C.
  7. Procédé selon la revendication 1, dans lequel le temps de séjour pendant l'oligomérisation est compris entre 0,5 et 8 heures.
  8. Procédé selon la revendication 1, dans lequel le solvant est choisi parmi les hydrocarbures paraffiniques C5 à C19.
  9. Procédé selon la revendication 1, dans lequel la conversion du monomère en polyalphaoléfine est supérieure à 95%.
  10. Procédé selon la revendication 1, dans lequel l'oligomérisation comprend des dimères C20-24, des trimères C30-36, des tétramères C40-48, des pentamères C50-60 et des lourds C60+.
EP21168133.3A 2020-04-14 2021-04-13 Procédé de contrôle de la viscosité cinématique d'une polyalphaoléfine Active EP3896141B1 (fr)

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EP3896141A1 (fr) 2021-10-20
CN113528214B (zh) 2023-07-11
CN113528214A (zh) 2021-10-22
US20210317380A1 (en) 2021-10-14
US11370987B2 (en) 2022-06-28

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